Method and installation for thermochemical conversion of raw material containing organic compounds

ABSTRACT

The invention relates to the field of organic substance processing, in particular to the method for processing the shredded wood waste, plant industry products, food industry waste, livestock and poultry waste. Products obtained during the thermal processing of organo-containing raw materials can be used as a fuel. The method comprises drying, hermetic supply of raw materials to the pyrolysis reactor, thermal decomposition of raw materials without air access in the pyrolysis reactor to produce solid products and vapour-gas mixture, the subsequent separation of it by condensation into liquid products and gaseous products. After drying, the organo-containing raw material before supply into the pyrolysis reactor is preheated to a temperature close to, but not exceeding the initiation temperature of thermal decomposition of the least thermally stable component of organo-containing materials Surfaces of the chamber are heated to a temperature which excludes the condensation of pyrolysis vapour-gas products, and raw material heating temperature is controlled by duration of stay in the preheating zone; Thermal decomposition is implemented in the form of the following successive stages occurring in corresponding zones of the pyrolysis reactor, having the possibility of independent temperature control: primary pyrolysis zone, vapour-gas mixture purification zone, secondary pyrolysis zone The installation for thermochemical conversion of organo-containing raw materials comprises a drying chamber, a hermetic raw material supply chamber, a pyrolysis reactor, a device for independent and elastic setting of the inclination angle of blades, a condensation unit. The pyrolysis reactor have a surface rotating with at least one blade and a rotation axis coinciding with the longitudinal axis of the pyrolysis reactor, and at least one ablation surface of circular or elliptical section, perpendicular to the rotation axis of the rotating surface. The hermetic raw material supply chamber is equipped with raw material heating means. The pyrolysis reactor workspace is divided along the path of raw materials into the following successive zones equipped with independent heating devices—a primary pyrolysis zone, a vapour-gas cleaning zone, equipped with a device for separation and return of incomplete destruction products, and a secondary pyrolysis zone. The use of the claimed group of inventions allows increasing the efficiency of the process of thermochemical conversion of organo-containing raw materials.

FIELD OF THE INVENTION

The invention relates to the field of organic substance processing, inparticular to the method for processing the shredded wood waste, plantindustry products, food industry waste, livestock and poultry waste.Products obtained during the thermal processing of organo-containing rawmaterials can be used as fuel.

BACKGROUND

In prior art there is a known method for ablative pyrolysis in avertical cylindrical tank with a rotating rotor inside it which islocated coaxially with the tank and have blades providing heating of rawmaterial due to the contact with heated walls of the tank, with theoutput of solid fractions and steam through holes located near the tankbottom. (No. U.S. Pat. No. 8,128,717 B2, Mar. 6, 2012—Mechanicallydriven centrifugal pyrolyzer.

The disadvantage of this method is the impossibility of ensuring thesame residence time of raw material particles in the reaction zone, thatis, ensuring the same degree of raw material destruction and stablequality of the products obtained. In addition, the contact of rawmaterial particles entering the reactor with ascending streams ofvapour-gas degradation products being formed, as well as the partialcondensation of these vapours on raw material particles lead to stickingof particles, clogging up of the space between blades and the rotor withthe resulting mass, exclude the possibility of providing the necessarycontact of the raw material with heated tank walls, make the heatexchange more difficult and thus eliminate the smooth operation andstable quality of resulting products.

Also, in the prior art there is a known method for ablative thermolysis,including hermetic supply of raw material particles, ablativethermolysis of raw material particles sandwiched between a rotatingsurface and a heated ablation surface, when raw material particles aremoving during thermolysis along the ablation surface using the rotatingsurface, output of thermolysis products. (US 2005/0173237 A1, August2005—Ablative thermolysis reactor.

Disadvantages of the prior art method are the difficulty of controllingthe speed of raw material particles' axial movement and the requiredtime of contact of raw material particles with the heated ablationsurface and, therefore, the impossibility of ensuring stable quality ofthe products obtained, as well as the possibility of sticking andaccumulation of particles between the rotating surface and the ablationsurface with the formation of an annular plug between the rotatingsurface and the shaft. Sticking and accumulation of raw materialparticles occurs as a result of the contact of colder particles of theraw material entering thermolysis area with vapour-gas reactionproducts, and their partial condensation on the surface of particles.Such an accumulation can lead to the termination of the process andjamming of the device. In addition, it is extremely difficult to choosea material that ensures the stable operation of an elastic element attemperatures from 450 to 700° C., since the operating temperature rangeof structural materials providing elasticity is much less than 500° C.

The combination of the above factors leads to low efficiency andreliability of the design.

The closest method in regards to technical essence and achieved resultis a method for thermal processing of organo-containing raw materials(RU No. 2395559, July 27, 2010), wherein the thermochemical conversionof organo-containing raw materials into gaseous and liquid fuels isimplemented by heating first in the drying chamber by a drying agentwith a temperature of 160-200° C., obtained by mixing flue gases thathave passed through the pyrolysis chamber sleeve with air, and then bythermal decomposition without air access in the pyrolysis reactor toproduce solid pyrolysis products and a vapour-gas mixture, withsubsequent condensation of a part of the vapour-gas mixture into fluidfuel, wherein a part of the uncondensed vapour-gas mixture afterpreheating to a temperature of 450-520° C. is fed into the pyrolysisreactor in an amount that ensures the residence time of pyrolysisproducts in the pyrolysis chamber not more than 2 seconds and the excesspressure in the pyrolysis chamber at the level of 500-1000 Pa.

Disadvantages of this method are as follows: additional heat consumptionfor heating a part of the uncondensed vapour-gas mixture, which afterthe condensation of liquid fuel is supplied to the pyrolysis chamber;significant fluctuations in the residence time of raw material particlesin the pyrolysis chamber, controlled by the amount of supplied recycledgas; gumming of parts of the power generation device with the exhaustpart of the uncondensed vapour-gas mixture; and even higher sticking ofraw material particles at the entrance to the pyrolysis chamber as aresult of the circulation of fine mist of the dripping high-boilingliquid in a gas recirculation circuit, which leads to instability of thequality of raw material destruction products. In addition, the supply ofcirculating gas into the pyrolysis chamber leads to additionalentrainment of fine coal into the gas recirculation circuit, depositionof this coal on walls of ducts, reduction of the working section ofducts and even greater instability of the pyrolysis process. Thecombined selection of a solid product (carbonaceous residue) and avapour-gas mixture from the reactor leads to the adsorption ofcomponents of the vapour-gas mixture on the carbonaceous residue surfaceand a decrease in its quality.

SUMMARY

Object of the invention is to increase the stability and efficiency ofthe process of thermochemical conversion of organo-containing rawmaterials, to increase the installation reliability and the quality ofproducts.

Technical result of the claimed group of inventions is an increase inthe efficiency of the process of thermochemical conversion oforgano-containing raw materials, which consists in ensuringuninterrupted operation with consistently high quality of the productsobtained. The technical result is achieved by a method forthermochemical conversion of organo-containing raw materials, the methodcomprising drying of said raw material, hermetic supply of said rawmaterial into a pyrolysis reactor, thermal decomposition of said rawmaterial without air access in the pyrolysis reactor to produce solidproducts and a vapour-gas mixture, subsequent separation of saidvapour-gas mixture by condensation into liquid products (a condensedpart of the vapour-gas mixture) and gaseous products (an uncondensedpart of the vapour-gas mixture), wherein (i) after drying and beforesupply into the pyrolysis reactor, the organo-containing raw material ispreheated to a temperature close to, but not exceeding a thermaldecomposition initiation temperature of the least thermally stablecomponent of said organo-containing raw material; (ii) surfaces of achamber of the pyrolysis reactor are heated to a temperature whichexcludes condensation of the vapour-gas mixture, and a heatingtemperature of the raw material is controlled by duration of stay in apreheating zone; (iii) the thermal decomposition is implemented in aform of the following successive stages occurring in corresponding zonesof the pyrolysis reactor, said zones are configured to have anindependent temperature control: a primary pyrolysis, where the rawmaterial is converted into solid products and the vapour-gas mixture; apurification of the vapour-gas mixture, wherein after the primarypyrolysis the vapour-gas mixture is cooled to a temperature, under whicha condensate is formed from a part of the vapour-gas mixture, the formedcondensate is returned and mixed with the solid products and unreactedparts of the raw material; and a secondary pyrolysis, wherein the formedgaseous products together with the primary pyrolysis vapour-gas mixtureare returned to the purification stage, and solid products are withdrawnfrom the secondary pyrolysis zone, preventing their contact with theprimary pyrolysis vapour-gas mixture.

In a particular embodiment of the claimed technical solution, thecondensation is implemented in three successive stages: primary coolingof the vapour-gas mixture in the vapour-gas mixture purification zone ofthe pyrolysis reactor; condensation of the vapour phase in thecondenser; separation of an uncondensed part of the vapour-gas mixturefrom the dripping liquid with recirculation of a part of the gaseousproduct through the pyrolysis reactor cleaning zone.

In a particular embodiment of the claimed technical solution, theprimary pyrolysis is implemented mainly in the mode of mechanicalablation. In a particular embodiment of the claimed technical solution,zones of primary and secondary pyrolysis provide the possibility ofindependent purging with an inert gas or a gas having reducing oroxidizing properties heated to a required temperature.

The technical result is also achieved due to the fact that in theinstallation for thermochemical conversion of organo-containing rawmaterials, comprising a drying chamber, a hermetic raw material supplychamber, a pyrolysis reactor having a surface rotating with at least oneblade and a rotation axis coinciding with the longitudinal axis of thepyrolysis reactor, and at least one ablation surface of circular orelliptical section, perpendicular to the rotation axis of the rotatingsurface, a device of independent and elastic setting of the inclinationangle of blades, a condensation unit consisting of a mass transferapparatus and a separator, the hermetic raw material supply chamber isequipped with raw material heating means, and the pyrolysis reactorworkspace is divided along the path of raw materials into the followingsuccessive zones equipped with independent heating devices—a primarypyrolysis zone, a vapour-gas cleaning zone, equipped with a device forseparation and return of incomplete destruction products, and asecondary pyrolysis zone.

In a particular embodiment of the claimed technical solution, blades arehinged on the rotating surface of the pyrolysis reactor and have atleast one degree of freedom.

In a particular embodiment of the claimed technical solution, the devicefor independent and elastic setting of the inclination angle of bladeshas a kinematic connection with them, is removed from the hightemperature zone, is isolated from the impact of the vapour-gas mixturebeing formed and is capable of providing elastic pressure with requiredperiodicity and force in the direction towards both the ablation surfaceand the rotating surface.

In a particular embodiment of the claimed technical solution, theelasticity in the device for independent and elastic setting of theinclination angle of blades is achieved by pneumatic, mechanical,electromagnetic and other methods.

In a particular embodiment of the claimed technical solution, blades areplaced on the rotating surface of the pyrolysis reactor offset from eachother along the length and radius of the rotating surface, inparticular, along the helical line.

In a particular embodiment of the claimed technical solution, geometryof the ablation surface of the pyrolysis reactor is made in the form ofa helical surface with variable or constant pitch, wherein the helicalsurface can be made without gaps or by individual sections.

In a particular embodiment of the claimed technical solution, heatingdevices of each of the three zones of the pyrolysis reactor have thepossibility of independent temperature control.

In a particular embodiment of the claimed technical solution, thecondensation unit separator is connected by pipeline to the reactorcleaning zone.

BRIEF DESCRIPTION OF THE DRAWINGS

Details, features, and advantages of this group of inventions followfrom the below description of embodiments of the claimed technicalsolutions using the drawings which show:

FIG. 1 diagram of the installation for thermochemical conversion oforgano-containing raw materials

FIG. 2 schematic representation of the device for independent andelastic setting of the inclination angle of blades, implemented usingthe pneumatic method

FIG. 3 flow diagram of the fast pyrolysis process

In the figures, numbers denote the following positions:

1—drying chamber; 2—chamber for hermetic supply of raw materials;3—pyrolysis reactor; 4—device for independent and elastic setting of theinclination angle of blades; 5—device for separation and return ofincomplete destruction products; 6—condensation unit; 7—separator;8—firebox; 9—coal out-feed device; 10—blades; 11—pneumatic cylinders.

SUMMARY OF THE INVENTION

To solve the object, in the method for thermochemical conversion oforgano-containing raw materials, including drying, hermetic supply ofraw materials to the pyrolysis reactor, thermal decomposition of rawmaterials without air access in the pyrolysis reactor to produce solidproducts and vapour-gas mixture, the subsequent separation of it bycondensation into liquid products (a condensed part of the vapour-gasmixture) and gaseous products (an uncondensed part of the vapour-gasmixture), after drying the organo-containing raw material before supplyinto the pyrolysis reactor is preheated to a temperature close to, butnot exceeding the initiation temperature of thermal decomposition of theleast thermally stable component of organo-containing materials, whereinsurfaces of the chamber are heated to a temperature which excludes thecondensation of pyrolysis vapour-gas products, and raw material heatingtemperature is controlled by duration of stay in the preheating zone;thermal decomposition is implemented in the form of the followingsuccessive stages occurring in corresponding zones of the pyrolysisreactor, having the possibility of independent temperature control:

primary pyrolysis, during which thermochemical conversion of rawmaterials into solid products and vapour-gas mixture is implementedmainly in the mode of mechanical ablation, without excluding the use ofother methods,

purification of the vapour-gas mixture, which consists in its withdrawalfrom the primary pyrolysis zone, cooling to a temperature that ensuresthe vapour-gas mixture purification from a part of solid and unreactedproducts withdrawn with it, return and mixing of these products withsolid primary pyrolysis products,

and secondary pyrolysis, wherein vapour-gas products formed arewithdrawn together with the primary pyrolysis vapour-gas mixture throughthe zone and the installation for purification of the vapour-gas mixtureand removal of solid products from the pyrolysis chamber, excludingtheir contact with the primary pyrolysis vapour-gas mixture,

wherein zones of primary and secondary pyrolysis provide the possibilityof independent purging with an inert gas or a gas having reducing oroxidizing properties heated to a required temperature;

condensation is implemented in three successive stages: primary coolingof the vapour-gas mixture in the vapour-gas mixture purification zone ofthe pyrolysis reactor; condensation of the vapour phase in thecondenser; separation of an uncondensed part of the vapour-gas mixturefrom the dripping liquid with recirculation of a part of the gaseousproduct through the pyrolysis reactor cleaning zone.

The installation for thermochemical conversion of organo-containing rawmaterials includes a drying chamber (1), a chamber for hermetic supplyof raw materials (2), a pyrolysis reactor (3), a condensation unit (6)and a firebox (8). The drying chamber is connected by transport devicesthrough metering devices with the chamber for hermetic supply of rawmaterials and the firebox. In a particular embodiment, such transportdevices are screw conveyors (they are not conventionally shown in thediagram).

The condensation unit includes mass transfer devices located in series—acondenser and a separator.

The pyrolysis reactor workspace is divided into three zones: the firstzone along the path of raw materials—a primary pyrolysis zone, thesecond zone—a vapour-gas mixture purification zone equipped with adevice for separation and return of incomplete destruction products, andthe third zone—a secondary pyrolysis zone. The pyrolysis reactor isequipped with an ablation surface that is capable of independentlycontrolling the temperature in each zone.

The pyrolysis reactor is equipped: in the primary pyrolysis zone, with anozzle connecting the reactor to the chamber for hermetic supply of rawmaterials; in the purification zone, with pipes for withdrawal of thevapour-gas mixture after purification to the condenser and for supply ofa part of the gaseous product after the separator to cool the primarypyrolysis vapour-gas mixture; in the secondary pyrolysis zone—with acoal out-feed device.

The pyrolysis reactor is also equipped with a rotor, on the rotatingsurface of which blades are located with a gap in length and radius thathave a kinematic connection with the device for independent and elasticsetting of the inclination angle of blades. The device for independentand elastic setting of the inclination angle of blades is offset fromthe high temperature zone and isolated from impact of the resultingvapour-gas mixture. Independent elastic setting of the angle and forceof blades pressing can be done by mechanical, electromagnetic, pneumaticand other methods. In a particular embodiment, it is implemented usingthe pneumatic method with the help of pneumatic cylinders and adistributor.

For this purpose, in the installation for thermochemical conversion oforgano-containing raw materials, comprising a drying chamber, a hermeticraw material supply chamber, a pyrolysis reactor having a surfacerotating with at least one blade and a rotation axis coinciding with thelongitudinal axis of the pyrolysis reactor, and at least one ablationsurface of circular or elliptical section, perpendicular to the rotationaxis of the rotating surface, a device of independent and elasticsetting of the inclination angle of blades, a condensation unitconsisting of a mass transfer apparatus and a separator, the hermeticraw material supply chamber is equipped with raw material heating means,and the pyrolysis reactor workspace is divided along the path of rawmaterials into the following successive zones equipped with independentheating devices—a primary pyrolysis zone, a vapour-gas cleaning zone,equipped with a device for separation and return of incompletedestruction products, and a secondary pyrolysis zone, wherein blades arehinged on the rotating surface of the pyrolysis reactor and have atleast one degree of freedom; the device for independent and elasticsetting of the inclination angle of blades has a kinematic connectionwith them, is removed from the high temperature zone, is isolated fromthe impact of the vapour-gas mixture being formed and is capable ofproviding elastic pressure with required periodicity and force in thedirection towards both the ablation surface and the rotating surface;the elasticity in the device for independent and elastic setting of theinclination angle of blades is achieved by pneumatic, mechanical,electromagnetic and other methods; blades are placed on the rotatingsurface of the pyrolysis reactor offset from each other along the lengthand radius of the rotating surface, in particular, along the helicalline; geometry of the ablation surface of the pyrolysis reactor is madein the form of a helical surface with variable or constant pitch,wherein the helical surface can be made without gaps or by individualsections; heating devices of each of the three zones of the pyrolysisreactor have the possibility of independent temperature control; thecondensation unit separator is connected by pipeline to the reactorcleaning zone.

Heating of organo-containing raw materials after drying before supply tothe pyrolysis reactor in the chamber for hermetic supply of rawmaterials equipped with heating means to a temperature close to, but notexceeding the temperature of thermal decomposition of the leastthermally resistant component of organo-containing raw materials, allowspartially removing the raw material heating zone from the reactor,eliminating the possibility of condensation of vapour-gas mixtureproducts on raw material particles entering the reactor from the dryingbin, and increasing the efficiency of heat exchange in the reactor.

Wherein, surfaces of the hermetic supply chamber are heated to atemperature that prevents condensation of the pyrolysis vapour-gasproducts, which reduces the process efficiency and the quality of finalproducts. Control of the raw material preheating temperature byresidence time allows effectively using the method and installation forvarious types of raw materials and excluding thermal decomposition inthe chamber for hermetic supply of raw materials.

The thermal decomposition is implemented successively in three stages incorresponding zones of the pyrolysis reactor (primary pyrolysis zone,vapour-gas mixture purification zone, secondary pyrolysis zone), whichhave the possibility of independent temperature control, which allowsimplementing the conversion of organo-containing raw materials withmaximum efficiency and consistently high quality of final products, andimplementing purification of the vapour-gas mixture from volatile finecoal forming in the presence of the vapour-gas mixture a layer ofresinous unreacted product at the reactor outlet, its return to thereaction zone, thereby preventing a reduction in the cross section ofgas ducts, sticking and clogging of the installation assemblies,eliminating sorbtion of the vapour-gas mixture by carbonaceous residuelocated in the secondary pyrolysis, thereby increasing the reliabilityof the coal out-feed device and the quality of coal produced, as well asimproving the quality of liquid products.

The sequential arrangement of the pyrolysis reactor zones prevents theincoming raw materials from contact with thermal decomposition products,as well as the contact of coal in the secondary pyrolysis zone with theprimary pyrolysis vapour-gas mixture, which improves the quality of thecoal being fed out by reducing the content of products of secondaryvapour-gas mixture decomposition.

The condensation implemented in three successive stages (primary coolingof the vapour-gas mixture in the vapour-gas mixture purification zone ofthe pyrolysis reactor; condensation of the vapour phase in thecondenser; separation of an uncondensed part of the vapour-gas mixturefrom the dripping liquid with recirculation of a part of the gaseousproduct through the pyrolysis reactor cleaning zone) allows increasingthe efficiency of separation of products being condensated and drippingliquids from gaseous products, excluding catalytic acceleration of theresinification reaction in the vapour-gas mixture, reducing thetemperature gradient in the condenser by supplying the vapour-gasmixture cooled in the pyrolysis reactor purification zone, increasingthe efficiency of further use of gaseous products, in particular togenerate electricity by reducing the content of dripping liquid.

The primary pyrolysis implemented in the mode of mechanical ablationallows reducing the requirements for particle size, in particular,allows processing particles up to 50 mm in size, reducing the cost forpreliminary grinding of raw materials.

Independent purging by an inert gas or a gas with reducing or oxidizingproperties heated to the required temperature in the primary andsecondary pyrolysis zones allows improving the conditions of primarypyrolysis and the quality of coal. Purging by inert gas eliminates theeffects of air entering the reaction zone, thereby increasing theinstallation safety. Purging by gas with reducing properties allowsincreasing the carbon content in the coal produced by converting some ofsubstances adsorbed by the coal into carbon. Purging by gas withoxidizing properties allows the activation process of coal, improvingporosity and sorption capacity, which will also improve its quality.

The hinge fixing of blades on the rotating surface of the pyrolysisreactor and providing them with at least one degree of freedom allowsself-regulating and reliable pressing of particles to the ablationsurface depending on various parameters (particle size of raw materials,etc.) during operation, as well as to the rotation surface duringperiodic cleaning.

The removal of the device for independent and elastic setting of theinclination angle of blades from the high temperature zone and itsisolation from the aggressive impact of the resulting vapour-gas mixtureensures uninterrupted stable operation of the reactor and theinstallation as a whole, as well as the pyrolysis process reliability.

Ensuring the possibility of elastic pressing of a blade with therequired periodicity both to the ablation surface and to the rotatingsurface allows for periodic high-quality cleaning of the reactorassemblies from raw material particles during continuous operation.

Location of blades on the rotating surface of the pyrolysis reactoroffset from each other along the length and radius of the rotatingsurface, in particular, along the helical line, as well as making thesurface geometry of the pyrolysis reactor ablation in the form of ahelical surface with variable pitch allow providing the controlled axialmovement of raw material particles along the pyrolysis reactor ablationsurface.

Thus, the proposed method allows increasing the stability and efficiencyof the process of thermochemical conversion of organo-containing rawmaterials, and increasing the installation reliability and the qualityof products.

The installation works as follows. Organo-containing raw material entersthe drying chamber (1), where moisture is removed from it to achieve amoisture content of not more than 10% abs. wt. Drying is implemented bya drying agent obtained by mixing flue gases from the pyrolysis reactorsleeve (3) with air. The dried organo-containing raw material enters thechamber for hermetic supply of raw materials (2), where it is heated tothe temperature at which thermal decomposition begins. In a particularembodiment, heating to the temperature of thermal decomposition isimplemented through the wall by flue gases from the reactor. Wherein,surfaces of the chamber for hermetic supply of raw materials can beheated significantly above the temperature of thermal decomposition toprevent condensation of vapour-gas products, and the heating of rawmaterials is controlled by duration of stay in the chamber.

Particles of the heated raw material entering the pyrolysis reactor (3),despite the polydisperse composition, are firmly pressed by blades ofthe rotating surface to the hot ablation surface, as a result of whichthe thermochemical conversion of organo-containing raw materials occurs.Pressuring of raw material particles by blades is ensured by means ofthe device (4), wherein the kinematic connection of pneumatic cylinderswith blades is provided by coaxial shafts as the option of a specificembodiment. Wherein, the device (4), which includes a pneumaticdistributor and pneumatic cylinders, is withdrawn from the hightemperature zone and is isolated from the impact of the vapour-gasmixture being formed (FIG. 2).

The ablation surface geometry in the form of a helical line and thearrangement of blades along the helical line provide the axialdisplacement of solid particles of the raw material set by the helicalline pitch and the rotor speed. Since the amount of solid particlesdecreases during the thermochemical conversion of the feedstock, theprocess stability along the pyrolysis reactor (3) axis is ensured by thevariable pitch of the helical line along the reactor length and thecontrolled force of pressing the blades. After the raw material haspassed the primary pyrolysis zone, the resulting vapour-gas mixture witha certain amount of volatile fine carbonaceous residue, formed as aresult of a fairly intensive mechanically activated treatment(ablation), enters the device for separation and return of incompletedestruction products (5).

The finely dispersed volatile coal in the form of a resinous unreactedproduct (products of interaction) accumulated on walls of the device forseparation and return of incomplete destruction products (5) saturatedwith vapour and partially condensed by decomposition products returnswith the remaining solid carbonaceous residue into the secondarypyrolysis zone for calcining and further through the coal out-feeddevice 9 into a coal collector. The vapour-gas mixture purified fromincomplete destruction products is fed to the condensation unit (6) forcondensation (condenser) and for separation of the droplet-phasecondensate in the form of a mist from non-condensable gas (separator).Wherein, the separator can be either of inertial type or in the form ofan electrostatic precipitator. Then, a part of cooled gaseous productsis fed by a fan to the vapour-gas mixture purification zone of thepyrolysis reactor (3).

Mixing of a hot vapour-gas mixture with cooled gaseous products promotesvolumetric condensation of vapours, coagulation and precipitation ofcondensate droplets and particles of fine volatile coal on workingsurfaces of the device for separation and return of incompletedestruction products in the form of a resinous unreacted product(interaction products). Interaction products periodically, but duringcontinuous operation of the pyrolysis reactor (3), are forciblyseparated from walls and other structural elements of the device forseparation and return of incomplete destruction products (5) andreturned to the pyrolysis reactor.

In a particular case, independent heating of each zone of the pyrolysisreactor is performed by feeding flue gases obtained by burning fuel inthe furnace (8) into the reactor sleeve, after mixing them with air toprovide the necessary temperature conditions for the pyrolysis process.After passing through the pyrolysis reactor (3) sleeve and mixing withair, flue gases are first fed into the chamber for hermetic supply ofraw materials to heat them to a temperature close to, but not exceedingthe temperature of thermal decomposition of the least thermallyresistant component of the organo-containing material, and then to thedrying chamber—as a drying agent. Below, we list the main operatingparameters and design characteristics for wood raw materials, as aspecific use of the method and installation for thermochemicalconversion of organo-containing raw materials.

No. Parameter Value 1. Temperature in the drying chamber 110 . . . 120°C. 2. Temperature in the chamber for 220 . . . 350° C. hermetic supplyof raw materials 3. Temperature in the primary pyrolysis 450 . . . 500°C. zone of the pyrolysis reactor 4. Temperature in the zone ofvapour-gas 100-490 . . . 520° C. mixture purification of the pyrolysisreactor 5. Temperature in the calcining zone of the 520 . . . 700° C.pyrolysisreactor 6. Temperature in the condensation unit, 30 . . . 50°C. not more than 7. Particle size of raw materials up to 50 mm

1. A method for thermochemical conversion of an organo-containing rawmaterial, comprising: drying of said raw material, hermetic supply ofsaid raw material into a pyrolysis reactor, thermal decomposition ofsaid raw material without air access in the pyrolysis reactor to producesolid products and a vapour-gas mixture, subsequent separation of saidvapour-gas mixture by condensation into liquid products (a condensedpart of the vapour-gas mixture) and gaseous products (an uncondensedpart of the vapour-gas mixture), wherein (i) after drying and beforesupply into the pyrolysis reactor, the organo-containing raw material ispreheated to a temperature close to, but not exceeding a thermaldecomposition initiation temperature of the least thermally stablecomponent of said organo-containing raw material; (ii) surfaces of achamber of the pyrolysis reactor are heated to a temperature whichexcludes condensation of the vapour-gas mixture, and a heatingtemperature of the raw material is controlled by duration of stay in apreheating zone; (iii) the thermal decomposition is implemented in aform of the following successive stages occurring in corresponding zonesof the pyrolysis reactor, said zones are configured to have anindependent temperature control: a primary pyrolysis, where the rawmaterial is converted into solid products and the vapour-gas mixture; apurification of the vapour-gas mixture, wherein after the primarypyrolysis the vapour-gas mixture is cooled to a temperature, under whicha condensate is formed from a part of the vapour-gas mixture, the formedcondensate is returned and mixed with the solid products and unreactedparts of the raw material; and a secondary pyrolysis, wherein the formedgaseous products together with the primary pyrolysis vapour-gas mixtureare returned to the purification stage, and solid products are withdrawnfrom the secondary pyrolysis zone, preventing their contact with theprimary pyrolysis vapour-gas mixture.
 2. The method according to claim1, wherein the condensation is implemented in three successive stages:primary cooling of the vapour-gas mixture in the vapour-gas mixturepurification zone of the pyrolysis reactor; condensation of a vapourphase in a condenser; separation of an uncondensed part of thevapour-gas mixture from a dripping liquid with recirculation of a partof the gaseous product through a pyrolysis reactor cleaning zone.
 3. Themethod according to claim 1, wherein the primary pyrolysis isimplemented in the mode of a mechanical ablation.
 4. The methodaccording to claim 1, wherein zones of primary and secondary pyrolysisare configured to provide an independent purging of the raw materialwith an inert gas or a gas having reducing or oxidizing properties, saidgases are heated to a required temperature.
 5. An installation forthermochemical conversion of organo-containing raw materials, comprisinga drying chamber, a hermetic raw material supply chamber, a pyrolysisreactor having a surface rotating with at least one blade and a rotationaxis coinciding with the longitudinal axis of the pyrolysis reactor, andat least one ablation surface of circular or elliptical section,perpendicular to the rotation axis of the rotating surface, a device ofindependent and elastic setting of the inclination angle of blades, acondensation unit consisting of a mass transfer apparatus and aseparator, wherein the hermetic raw material supply chamber is equippedwith raw material heating means, and the pyrolysis reactor workspace isdivided along the path of raw materials into the following successivezones equipped with independent heating devices—a primary pyrolysiszone, a vapour-gas cleaning zone, equipped with a device for separationand return of incomplete destruction products, and a secondary pyrolysiszone.
 6. The installation according to claim 5, wherein blades arehinged on the rotating surface of the pyrolysis reactor and have atleast one degree of freedom.
 7. The installation according to claim 5,wherein the device for independent and elastic setting of theinclination angle of blades has a kinematic connection with them, isremoved from the high temperature zone, is isolated from the impact ofthe vapour-gas mixture being formed and is capable of providing elasticpressure with required periodicity and force in the direction towardsboth the ablation surface and the rotating surface.
 8. The installationaccording to claim 5, wherein the elasticity in the device forindependent and elastic setting of the inclination angle of blades isachieved by pneumatic, mechanical, electromagnetic and other methods. 9.The installation according to claim 5, wherein blades are placed on therotating surface of the pyrolysis reactor with offset from each otheralong the length and radius of the rotating surface, in particular,along the helical line.
 10. The installation according to claim 5,wherein geometry of the ablation surface of the pyrolysis reactor ismade in the form of a helical surface with variable or constant pitch,wherein the helical surface can be made without gaps or by individualsections.
 11. The installation according to claim 5, wherein heatingdevices of each of the three zones of the pyrolysis reactor have thepossibility of independent temperature control.
 12. The installationaccording to claim 5, wherein the condensation unit separator isconnected by pipeline to the reactor cleaning zone.